Solvent extraction of oil from distillers dried grains and methods of using extraction products

ABSTRACT

A process for extraction of crude oil from DDGS and producing corn distillers meal that may be used as a livestock supplement is disclosed. For example, the corn distillers meal may be used as a crude protein supplement for use in a livestock feed diet or a poultry feed diet.

This application is a continuation of U.S. application Ser. No.12/442,934, filed on Mar. 25, 2009, which is a National Stage Filingunder 35 U.S.C. 37 of International Application No. PCT/US2007/079575,filed Sep. 26, 2007, which designated the United States and which claimsthe benefit of U.S. Provisional Application No. 60/847,188, filed Sep.26, 2006. This application hereby incorporates by reference the U.S. andinternational priority application and patents enumerated herein.

TECHNICAL FIELD

This disclosure relates generally to the extraction of oil fromdistillers dried grains with solubles (DDGS) to produce distillers meal,methods of using the oil extracted from DDGS, and methods of using thedistillers meal as a feed supplement for animal feed. More particularly,described herein are methods for solvent extraction of crude oil fromDDGS to provide distillers meal having a desired nutrient content,methods of processing the crude oil extracted from the DDGS to provideoil suitable for consumer use, methods of processing the crude oilextracted from the DDGS in a biodiesel production process, and methodsof using the distillers meal as an animal feed supplement.

STATE OF THE ART

Ethanol can be produced using grains, such as corn, which are renewableresources. Presently, the majority of ethanol-producing biorefineries inthe United States are dry-grind corn biorefineries, and it is estimatedthat the present ethanol production capacity of such biorefineries runsinto the billions of gallons each year. Co-products of the ethanolbiorefining process are distillers dried grains and distillers driedgrains with solubles. Based on current production rates of ethanol fromdry-grind ethanol plants, approximately 12 million tons of DDGS areproduced in the United States annually. It is also estimated that thisnumber could grow to 18 to 20 million tons per year within the next fewyears.

Over the past few decades, achieving an ethanol product from grain-basedbiorefineries that is both commercial viable and truly renewable hasproven challenging. Two of the more significant hurdles are: 1) the costof grain-based ethanol production; and 2) the energy input to outputratio of grain-based ethanol production processes. As is easilyappreciated, these two problems are intertwined. Grain-based ethanolproduction has historically required significant and costly input offossil fuels (e.g., natural gas) to drive the biorefining process.Moreover, the amount of fossil fuel that has been historically requiredto drive grain-based ethanol production is costly, particularly so asthe cost of natural gas and other fossil fuels increases.

One of the ways by which the effective cost of grain-based ethanolproduction can be reduced is the sale of commercially valuableco-products of the biorefining process. DDGS are co-products ofgrain-based ethanol production processes that have recognized commercialvalue. In particular, DDGS are sold as a livestock feed supplement.Because it is primarily the starch of the grain that is consumed in theproduction of ethanol, the DDGS remaining after fermentation anddistillation contain nutritionally valuable fiber, protein and fat.Relative to raw grain, DDGS may even be considered a superior feed, asthey contain concentrated amounts of fiber, protein and fat, togetherwith a significantly reduced amount of starch. In addition, DDGS areconsiderably less expensive than some feeds of comparable nutritionalvalue.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 provides a flow-chart representation of the process by whichcrude oil is extracted from DDGS and refined into biodiesel andglycerin.

FIG. 2 provides a flow-chart representation of the process by whichbiodiesel and glycerin are produced from oil extracted from DDGS.

DETAILED DESCRIPTION

It will be readily understood that the methods and materials as they aregenerally described and illustrated in the figures herein could bearranged and designed in a wide variety of different configurations.Thus, the following more detailed description of various embodiments ofthe methods and materials provided herein is not intended to limit thescope of the claims, but merely provides representative examples ofvarious embodiments of the subject matter recited in the appendedclaims. For example, though DDGS are referenced herein with respect tothe methods and materials described, it is to be understood thatdistillers dried grains (DDG) could also be utilized. In particular, DDGretain significant oil content, and in embodiments of the processes andmethods described herein DDG may be used in place of DDGS. Moreover, DDGretain valuable nutrient properties and distillers meal, resulting fromsolvent extraction of DDG according to the methods described herein, mayalso be utilized as an animal feed supplement.

As is described herein, the commercial value of DDG and DDGS fromgrain-based ethanol production processes can be further enhanced. Inparticular, commercially valuable amounts of oil can be extracted fromthe DDG and DDGS using a solvent extraction process. The solventextracted oil can then be further processed to provide, for example,food grade oil, such as food grade corn oil where the DDG and DDGS arederived from an ethanol biorefinery that utilizes corn grain as biomass.Alternatively, the oil extracted from DDG and DDGS can be subjected to atransesterification process to yield biodiesel and glycerin. Thedistillers meal resulting from solvent extraction as described herein isstill suitable for use as an animal feed, such as, for example, a feedsupplement or constituent for domestic pets, livestock or poultry.Therefore, solvent extraction of DDG and DDGS according to the methodsdescribed herein may facilitate a reduction in the effective costs ofproducing ethanol from a grain-based biorefinery, as it allows forproduction of multiple, commercially-valuable products from DDG andDDGS.

In one embodiment, ethanol production, solvent extraction of DDGS, andrefining of the crude oil removed from the DDGS can occur in a singlefacility. For example, in such an embodiment, a grain-based ethanolbiorefinery may further include facilities for solvent extraction of theDDGS produced at the biorefinery. In another such embodiment, agrain-based ethanol biorefinery may further include facilities forsolvent extraction of the DDGS produced at the biorefinery andfacilities for processing the crude oil extracted from the DDGS toprovide a food-grade oil suitable for consumer use. In yet anotherembodiment, a grain-based ethanol biorefinery may further includefacilities for solvent extraction of the DDGS produced at thebiorefinery and facilities for processing and refining the crude oilextracted from the DDGS to produce biodiesel and glycerin. Byintegrating these operations within a single facility, processefficiencies may be gained and costs of solvent extracting the DDGS andprocessing or refining the extracted oil may be reduced.

Solvent Extraction of Crude Oil from DDGS

Using solvent extraction processes, commercially significant amounts ofcrude plant oils can be isolated from DDGS, while maintaining the valueof DDGS as a feed supplement. In one embodiment, the DDGS used in asolvent extraction process as described herein are selected from DDGSgenerated in ethanol production processes that utilize corn, barley,rye, or soybean grain. In another embodiment, the DDGS used in a solventextraction process are corn DDGS generated from a dry-grind corn ethanolbiorefinery.

Solvent extraction processes suitable for extraction of crude oil fromDDGS include processes that utilize ethanol, hexane, iso-hexane,petroleum distillate, mixtures thereof, or one or more other suitablesolvents, as known in the art, for oil extraction of DDGS. In oneembodiment, the solvent extraction process utilizes a solvent, such as,for example, hexane, that serves to remove oil from the DDGS withoutsubstantially altering the protein or fiber content of the DDGS. Oilextraction of the DDGS as described herein yields a distillers meal. Inone embodiment, the solvent extraction process removes about 75% ormore, about 80% or more, or about 90% or more of the oil present in theDDGS. In another embodiment, the solvent extraction process is a hexaneextraction process that removes about 75% or more, about 80% or more, orabout 90% or more of the oil present in the DDGS. In yet anotherembodiment, the solvent extraction process is a hexane extractionprocess that removes about 75% or more, about 80% or more, or about 90%or more of the oil present in corn DDGS. In yet another embodiment, thesolvent extraction process is a hexane extraction process that removesabout 75% or more, about 80% or more, or about 90% or more of the oilpresent in DDGS produced at a dry-grind corn ethanol biorefinery. CornDDGS typically include 10-15% by weight oil content, and in oneembodiment, the solvent extraction process is a hexane extractionprocess that results in a corn distillers meal having a residual oilcontent of approximately 2-3% by weight. In another embodiment, cornDDGS are subjected to a hexane extraction process that results in a corndistillers meal having a residual oil content of no more than 2.5% byweight.

Where the DDGS are produced at a dry-grind corn ethanol biorefinery, aflow-chart representation of suitable hexane extraction process is shownin FIG. 1. In a typical dry-grind process for ethanol production fromcorn, the DDGS are a co-product derived from the corn mash after thestarch has been converted to ethanol and the ethanol has been removed bydistillation. The stillage is typically subjected to centrifugation,evaporation and drying to remove residual liquid content, resulting inDDGS. Methods of extracting crude corn oil from corn DDGS are discussedin Sing et. al., “Extraction of Oil From Corn Distillers Dried Grainswith Solubles”, Transactions of the ASAE 41 (6), 1775-1777 (1998), theteachings of which are incorporated by reference herein. In addition,solvent extraction technologies and equipment are available from, forexample, Crown Iron Works Company of Minneapolis, Minn., U.S.A.Moreover, technology directed to removal of the oil from vegetableparticles, removal of residual solvent from solvent extracted materials,and recovery of solvents used in solvent extraction processes aredescribed in, for example, U.S. Pat. No. 6,996,917, U.S. Pat. No.6,766,595, U.S. Pat. No. 6,732,454, and U.S. Pat. No. 6,509,051. Thesepatents are assigned to Crown Iron Works Company, and the teachings ofeach of these patents are incorporated by reference herein.

Referring again to FIG. 1, which illustrates an embodiment of a solventextraction process that may be applied to DDGS, as a first step, DDGSmeal is fed into an extractor. In the extractor, the DDGS meal is washedwith solvent, and in one embodiment, the DDGS meal is turned at leastonce in order to ensure that all sides of the DDGS particles are washedwith solvent. After washing, the resulting mixture of oil and solvent,called miscella, is collected for separation of the extracted oil fromthe solvent. During the extraction process, as the solvent washes overthe DDGS flakes, the solvent not only brings oil into solution, but itcollects fine, solid DDGS particles. These “fines” are generallyundesirable impurities in the miscella, and in one embodiment, themiscella is discharged from the separator through a device thatseparates or scrubs the fines from the miscella as the miscella iscollected for separation of the oil from the solvent.

In order to separate the oil and the solvent contained in the miscella,the miscella may be subjected to a distillation step. In this step, themiscella can, for example, be processed through an evaporator, whichheats the miscella to a temperature that is high enough to causevaporization of the solvent, but is not sufficiently high to adverselyaffect or vaporize the extracted oil. As the solvent evaporates, it maybe collected, for example, in a condenser, and recycled for future use.Separation of the solvent from the miscella results in a stock of crudeoil, which may be further processed to provide, for example, food gradeoil for consumer use or an oil product suitable for use in atransesterification process that yields biodiesel and glycerin.

After extraction of the oil, the wet, de-oiled DDGS may be conveyed outof the extractor and subjected to a drying process that removes residualsolvent. Removal of residual solvent is important to production ofdistillers meal suitable for use as an animal feed supplement. In oneembodiment, the wet meal can be conveyed in a vapor tight environment topreserve and collect solvent that transiently evaporates from the wetmeal as it is conveyed into the desolventizer. As the meal enters thedesolventizer, it may be heated to vaporize and remove the residualsolvent. In order to heat the meal, the desolventizer may include amechanism for distributing the meal over one or more trays, and the mealmay be heated directly, such as through direct contact with heated airor steam, or indirectly, such as by heating the tray carrying the meal.The desolventizer may further include multiple different trays forcarrying the meal through different processing steps within thedesolventizer. In order to facilitate transfer of the meal from one trayto another, the trays carrying the meal may include openings that allowthe meal to pass from one tray to the next.

Where the desolventizer utilizes multiple process steps to removeresidual solvent from the wet, de-oiled DDGS to produce distillers meal,the wet, de-oiled DDGS may be loaded and transferred through varioustrays to facilitate heating and solvent removal in multiple processsteps. For example, in one embodiment, as the meal enters thedesolventizer, it may be loaded on a first group of heated trays wherethe flakes are evenly distributed and solvent vapor is flashed from themeal. From this first set of trays, the meal may be transferred onto asecond group of trays, where it is again evenly distributed. The secondset of trays may be heated indirectly by steam. The trays may bedesigned to allow venting of the solvent from one tray to the next andthe meal contained in the second set of trays travels counter current tothe solvent vapors. A third tray or set of trays may be provided toallow direct steam injection into the meal, which works to stripremaining solvent. Where the desolventizer includes multiple trays andutilizes multiple drying processes, the quantity of trays and theirpositions may be designed to allow maximum contact between vapors andmeal.

From the desolventizer, the meal may be conveyed to a dryer where themeal is dried of residual water and cooled to provide a finisheddistillers meal. As it is conveyed into the dryer, the meal may bedeposited into drying trays and it is warmed by heated air. As the mealis heated, residual water and remaining solvent are vaporized. Afterdrying, the meal may be cooled using ambient air. The desolventized,dried and cooled distillers meal may be stored, further processed, orprepared for sale or distribution.

The biorefining and solvent extraction processes may be tailored toprovide extracted oil exhibiting specific qualities. For example, wherethe DDGS are corn DDGS and the solvent extraction process is a hexaneextraction process, the biorefining and solvent extraction process maybe controlled to provide an extracted crude corn oil exhibiting no morethan about 15% by weight free fatty acids, such as oleic acid, no morethan about 1% by weight crude protein, 0.5% by weight total nitrogen,0.2% by weight ash, 0.05% phosphorus, 0.05% by weight potassium, 0.01%by weight potassium, 0.005% sodium, or 0.05% by weight sulfur, or anycombination of one or more such qualities. In one such embodiment, thecrude corn oil includes no more than about 0.6%, 0.7%, 0.8% or 0.9% byweight crude protein. In another such embodiment, the crude oil containsno more than about 10%, 11%, 12%, 13%, 14%, or 15% by weight free fattyacids. In another such embodiment, the crude corn oil contains no morethan about 0.09%, 0.1%, 0.2%, 0.3%, or 0.4% by weight total nitrogen. Inyet another such embodiment, the crude corn oil contains no more thanabout 0.08%, 0.09%, 0.1%, or 0.15% by weight ash. In another suchembodiment, the crude corn oil contains no more than about 0.02%, 0.03%,or 0.04% by weight phosphorus. In yet another such embodiment, the crudecorn oil contains no more than about 0.02%, 0.03%, or 0.04% by weightpotassium. In yet another such embodiment, the crude corn oil containsno more than about 0.003% or 0.004% by weight sodium. In yet anothersuch embodiment, the crude corn oil contains no more than about 0.02%,0.03%, or 0.04% by weight sulfur.

Distillers Meal

The distillers meal produced by a solvent extraction method as describedherein retain desired nutritional properties. The solvent extractionprocess applied to the DDGS may be chosen and tailored to provide adistillers meal that exhibits nutritional properties suitable for animalfeed applications. For example, in one embodiment, the DDGS aresubjected to a solvent extraction process that provides distillers mealthat retains substantially all the crude protein and fiber content ofthe DDGS prior to solvent extraction. In another embodiment, thedistillers meal is corn distillers meal that retains substantially allof the crude protein and fiber content of the DDGS prior to solventextraction. In yet another embodiment, distillers meal is corndistillers meal that retains substantially all of the crude protein andfiber content of the DDGS prior to solvent extraction and is the productof a hexane extraction process conducted on corn DDGS produced by adry-grind corn ethanol biorefinery.

For example, where the DDGS are corn DDGS and the solvent extractionprocess is a hexane extraction, the biorefining and solvent extractionprocesses may be controlled to provide corn distillers meal having thefollowing nutrient content by weight on a dry matter basis: about 28% toabout 35% crude protein; about 4% to about 6% total nitrogen; about 1%to about 5% crude fat; about 4% to about 6% ash; about 5% to about 7%crude fiber; about 11.5% to about 13.5% acid detergent fiber; about 25%to about 35% neutral detergent fiber; about 50% to about 55% nitrogenfree extract; about 75% to about 80% total digestible nutrients (“TDN”);or a combination of two or more of any of the forgoing nutritionalproperties. In another embodiment, where the DDGS are corn DDGS and thesolvent extraction process is a hexane extraction, the biorefining andsolvent extraction processes may be controlled to provide corndistillers meal exhibiting about 0.80 to about 0.85 Mcal/lb net energylactation (NE/Lactation), about 0.85 to about 0.89 Mcal/lb net energymaintenance (NE/maintenance), about 1200 to about 1250 kcal/lb ofmetabolizable energy, or about 0.55 to about 0.60 Mcal/lb of net energygain (NE/gain), or any combination of two or more such characteristics.

The distillers meal may be further processed, as desired, to provide adistillers meal product having desired characteristics, such as, forexample, a desired flowabilty or density. Moreover, the distillers mealmay be further processed to provide a product that is more easilypackaged and distributed as a feed. Even further, the distillers mealmay be processed to incorporate additional constituents to increase thefeedability or nutritional quality. For example, in one embodiment, thedistillers meal may be further processed to incorporate a salt or asyrup from another manufacturing process that provides additionalprotein content. In another embodiment, the distillers meal may bepelleted to provide a feed material that is more readily packaged forsale and transport and is more easily incorporated into or used as ananimal feed. For instance, Example 2 provides a description of anembodiment of corn distillers meal according to the description providedherein, as well as suitable process conditions for pelletizing the corndistillers meal described therein. Tables presented in Example 2 set outthe process conditions under which the corn distillers meal waspelletized, describe a selection of physical properties exhibited by thenon-pelleted and the pelleted corn distillers meal, and highlight aselection of nutritional properties exhibited by the non-pelleted andthe pelleted corn distillers meal.

Further Processing of the Crude, Extracted Oil

After extraction from the DDGS, the crude oil may be further processedas desired. For example, the crude oil may be filtered and bleached toprovide a food grade oil for consumer use. For example, in oneembodiment, the crude oil may be degummed, caustic refined, andsubjected to a soap removal step according to commercially availableprocesses. Following these steps the oil may then be subjected to one ormore clay bleaching steps to achieve an oil of desired content andcolor. Where one or more clay bleaching steps are used, the clay may bean acid clay or a non-acid clay, and the bleaching step may include, byway of example, an acid clay or a non-acid clay at 1-5%, 2-4%, or 2-3%.In addition to or as an alternative to clay bleaching, after the crudeoil has been degummed, caustic refined and subjected to a soap removalstep, a food grade oil of a desired color may be achieved using a heatbleaching step. Suitable processes for degumming, caustic refining, andsoap removal are described herein in relation to the pretreatment stepsfor biodiesel and glycerin production from the crude oil. Clay bleachingand heat bleaching processes are also accessible to those of skill inthe art and can be utilized as described herein to achieve a food gradeoil.

Alternatively, the crude oil extracted from DDGS may be used to producebiodiesel and glycerin. A flow-chart representation of a process forrefining biodiesel and glycerin from the crude extracted oil is shown inFIG. 2. There are several processes that may be used to producebiodiesel from oils and fats, including base catalyzedtransesterification, direct acid catalyzed transesterification, andconversion of the oil to its fatty acids followed by conversion of thefatty acids to biodiesel. Biodiesel production technologies andequipment are commercially available from, for example, Crown Iron WorksCompany of Minneapolis, Minn., U.S.A., and from Lurgi AG of Frankfurt,Germany. To produce biodiesel and glycerin from the crude oil extractedfrom the DDGS, a base catalyzed transesterification process may be used.

In one embodiment, of the refining process outlined in FIG. 2, the crudeextracted oil is crude corn oil, and before the crude corn oil issubjected to a transesterification process, it may be pretreated.Pretreatment of the crude corn oil may be carried out, for example, toremove gums included in the oil or to remove or neutralize free fattyacids. As part of a degumming process, an acid, such as phosphoric acid,may be added to the crude corn oil and the crude oil may be heated, forexample, using steam. In such a process, the acid and steam work toswell the gums so that the gums can be separated from the crude cornoil, such as by centrifugation or another suitable separation technique.

Free fatty acids in the crude corn oil are generally undesirable becausethey tend to form soaps within the oil as they react with the basecatalyst used to drive the transesterification reaction. Where crudecorn oil is pretreated to neutralize free fatty acids, a strong base,such as NaOH (caustic soda) or KOH (potash) may be added to the crudecorn oil to neutralize free fatty acids. In combination with theaddition of a strong base, the crude corn oil may be heated, forexample, with steam. Such “steam stripping” can be useful in removingfree fatty acids from the oil phase. If the crude corn oil is alsopretreated with a degumming step, the addition of the strong baseintended to neutralize the free fatty acids may occur after addition ofthe acid in the degumming step. In this manner, the base added toneutralize the free fatty acids can also work to neutralize the acidused in the degumming step. The soap stock that results from degummingand neutralization of the crude corn oil may be separated from the cornoil using standard equipment, such as a centrifugal separator.Alternatively, the free fatty acids can be removed and acid esterifiedto form biodiesel, or combined with glycerin to form triglycerides,which are then transesterified to form biodiesel.

Pretreatment of the crude corn oil may also include one or morebleaching steps, such as one or more heat bleaching or clay bleachingsteps as described above, to remove residual color or other impuritiesfrom the corn oil.

Where pretreatment of the crude corn oil includes degumming andneutralization of free fatty acids, prior to a transesterificationprocess, the degummed and neutralized oil is typically washed prior totransesterification. Washing may include, for example, mixing thepretreated corn oil with warm wash water. After washing, the oil andwash water are separated, and the pretreated corn oil is dried, such asby a vacuum-dryer, to a desired water content.

In one embodiment, the pretreated corn oil can be subjected to atransesterification reaction to provide biodiesel and glycerin. Thetransesterification reaction is based on the chemical reaction oftriglycerides contained in the crude corn oil with an alcohol in thepresence of an alkaline catalyst. The alkaline catalyst used in thetransesterification reaction may be selected from several differentalkaline materials. Suitable catalysts are strong bases and include, forexample, NaOH (caustic soda), KOH (potash), and CH₃NaO (sodiummethylate). The alcohol used in the transesterification reaction may beselected from, for example, methanol or ethanol.

As the transesterification reaction is carried out, the alcohol andcatalyst may be delivered into the corn oil in parallel, as separatereaction components, or the alcohol and catalyst can be delivered to thecrude corn oil as a mixture. When delivered as a mixture, the catalystmay be dissolved in the alcohol by any suitable means prior to chargingthe mixture into the corn oil. Alternatively, the catalyst may beprovided as a liquid and mixed with the alcohol, limiting the need fordissolution of the catalyst in the alcohol prior to mixing the alcoholand catalyst with the corn oil. Where the catalyst is mixed with thealcohol as a liquid, the catalyst may be added to the alcohol by, forexample, one or more metering pumps. In addition, because an alkalinecatalyst might be sensitive to water, the catalyst may be stored in apump tank protected with a nitrogen layer.

In carrying out the transesterification reaction, the alcohol, catalystand corn oil may be charged into a closed reaction vessel. The reactionsystem can be closed to the atmosphere to prevent loss of the alcoholused in the transesterification reaction. As the reaction components aremixed, the mixture may be kept just below the boiling point of thealcohol to speed the reaction time. In addition, and excess amount ofalcohol is typically used to ensure total conversion of the corn oiltriglycerides into the desired ester product. The transesterificationreaction produces a two-phase reaction product that includes anester-rich phase (crude biodiesel) and a glycerin-rich phase (crudeglycerin). The crude glycerin is much more dense than the crudebiodiesel and the two phases can be easily separated by gravityseparation or, if needed or desired, centrifugation.

In one embodiment, transesterification of the corn oil takes place inone or more mixer-settler units. In such units, the transesterificationreaction occurs in a mixer or reactor included in the mixer-settlerunits. The crude biodiesel and crude glycerin resulting from thetransesterification reaction form two distinct phases that can beseparated in the settlers. If two or more mixer-settler units are usedas the reaction vessels, the feedstock and the intermediate product,respectively, may flow successively through the two or moremixer-settler units. Each mixer-settler unit can be supplied with thedesired alcohol and catalyst in parallel. The reactors included in themixer-settler units can be multi-stage in design, comprising variousreaction chambers in order to achieve maximum conversion efficiency tothe ester product. The settlers allow phase separation to approach thelimit of solubility, which eases downstream purification of thebiodiesel and glycerin products.

At the transesterification stage, vapors vented from the reactionvessel, such as the one or more mixer-settlers, may be routed to acondenser where they are partly or completely condensed and returned tothe reaction process. The same may be done with the vessel used to storeor deliver the alcohol used in the transesterification reaction. Evenfurther, where the catalyst is provided in liquid form, it too may bestored and delivered from a storage vessel, and any vapors vented fromthe catalyst storage vessel may also be captured, partly or completelycondensed, and returned to the reaction process in liquid form.

Once the transesterification reaction is complete, two major productsexist: glycerin and biodiesel. The glycerin is included in the crudeglycerin phase and the biodiesel is incorporated in the crude biodieselphase. Each of these crude phases may include a substantial excess ofthe alcohol used in the reaction. Moreover, the crude reaction productsmay include other impurities such as excess catalyst, soaps and highboiling impurities. If desired, some of these impurities may be treatedor removed from the crude reaction products before the crude biodieseland the crude glycerin phases are separated. For example, a suitableacid may be added to and mixed with the reaction products to neutralizeexcess catalyst. Additionally, excess alcohol may be removed from thecrude reaction products using standard distillation equipment andtechniques.

After the crude biodiesel and crude glycerin are separated, they aretypically subjected to further refining. For example, after separation,the crude biodiesel may contain residual alcohol, glycerin, smallamounts of catalyst, and soaps. This may be the case even if the crudereaction products are refined to remove or neutralize impurities priorto separation. If they have not already been refined to neutralizeexcess catalyst or remove excess alcohol, or if residual catalyst andexcess alcohol still remain in the separated reaction products, thecrude biodiesel and crude glycerin may be treated with a suitable acidto neutralize the residual catalyst and subjected to, for example, aflash evaporation process or distillation to remove the excess alcohol.

Even where steps are taken to neutralize residual catalyst and removeexcess alcohol, the refined biodiesel may still include water solubleimpurities. In order to remove such water-soluble substances, therefined biodiesel may be washed and dried. To avoid the formation ofemulsions during washing, soaps that may be present in the biodiesel maybe split, for example, by the addition of an acid to the biodiesel to bewashed. Dilute HCl, such as a 3.7% strength HCl, is suitable for such anapplication and can be prepared and added as necessary. The biodieselwash process may simply include gentle mixing of the biodiesel with warmwater, which will work to remove residual, water soluble impurities asthey are taken up in the aqueous phase.

If the biodiesel is processed through such a washing step, the refinedand washed biodiesel may contain excess water. Such excess water may beremoved, for example, by subjecting the biodiesel to a drying step. Thedrying step may include, for example, vacuum drying the biodiesel to adesired water content in a dryer circuit. The dried biodiesel, which isready for use, distribution or sale, is collected and stored. Though thebiodiesel is serviceable at this point, if desired, it can be subjectedto further distillation to remove any color bodies remaining to providea colorless biodiesel.

The separated, crude glycerin phase may also be further refined afterseparation. In particular, the crude glycerin may be neutralized with asuitable acid, the excess alcohol may be removed by distillation orflash evaporation, and the crude glycerin may be dried to removeresidual water. Even if the crude reaction products of thetransesterification process are neutralized and the excess alcoholpresent in the crude reaction products is removed prior to separation,the separated, crude glycerin may still contain residual catalyst oralcohol. Where that is the case, the separated, crude glycerin may besubjected to additional neutralization and distillation steps toneutralize any residual catalyst and remove any remaining alcohol. Oncesuch neutralization, distillation and drying steps are complete, thecrude product typically contains approximately 80-88% pure glycerin.This crude glycerin can be further refined to a purity of 99% or higher,as is known in the art, such that the glycerin product is suitable foruse in cosmetic or pharmaceutical applications.

In order to minimize loss of the alcohol used in the transesterificationreaction, all vessels which contain alcohol, whether in substantiallypure form or as part of a crude reaction product, may be connected to avent system to capture any alcohol vapors. Captured alcohol vapors maybe fed into a condensing system that recovers the alcohol and recyclesthe alcohol back into the refining process.

Distillers Meal as an Animal Feed

DDGS are often used as a feed supplement for livestock and poultry fedhigh grain content finishing diets. Before solvent extraction, DDGS mayhave approximately 30% by weight crude protein (“CP”) and 20% crudefiber (“CF”). Solvent extraction as described herein removes most of theoil from the DDGS so that such oil can be processed or refined toprovide additional products of commercial value. However, because mostof the oil present in DDGS is removed in producing distillers meal, theenergy potential of the distillers meal is significantly lower than thatexhibited by the DDGS prior to solvent extraction. Despite the lowerenergy potential resulting from oil extraction, distillers meal asdescribed herein provides a high-quality, low-cost feed for animals,such as domestic pets, livestock or poultry. In addition, as describedherein, livestock feed distillers meal exhibit desirable carcass traits,and the nutritional properties of distillers meal may provide a superiorfeed or feed supplement.

In one embodiment, the distillers meal disclosed herein may be used tosupplement animal diets at a desired percentage of the total diet, on adry matter basis. In one embodiment, the distillers meal may be used asa CP supplement in livestock and poultry feed diets. In addition, thedistillers meal described herein may also be used as an animal feed orfeed supplement that provides desired amounts of carbohydrates, fiber ornon-protein nitrogen (NPN) containing compounds. The de-distillers mealcan be used at a percentage of the total feed that maximizes thenutritional components of the feed. The relative amount of distillersmeal incorporated into an animal diet may depend on, for example, thespecies, sex, or agricultural use of the animal being fed. Additionally,the relative amount of distillers meal incorporated into a particulardiet may depend on the nutritional goals of the diet.

In one embodiment, distillers meal may be used to provide approximately50% to approximately 75% by weight, on a dry matter basis, of a totaldiet for use in an animal feed. In one such embodiment, the distillersmeal is corn distillers meal as described herein and is used to provideapproximately 50% to 55%, 50% to 60%, 50% to 65%, or 50% to 70% byweight, on a dry matter basis, of the total diet. In another suchembodiment, the distillers meal is corn distillers meal as describedherein and is used to provide approximately 50% to 55%, 55% to 60%, 55%to 70%, 60% to 65%, 60% to 70%, or 70% to 75% by weight, on a dry matterbasis, of the total diet.

In another embodiment, distillers meal as described herein may be usedto provide approximately 0 to 5%, approximately 5% to 10%, approximately5% to 15%, approximately 5% to 25%, approximately 5% to 30%,approximately 10% to 15%, approximately 15% to 20%, approximately 20% to25%, approximately 25% to 30%, approximately 30% to 35%, approximately35% to 40%, approximately 40% to 45%, or approximately 45% to 50% byweight, on a dry matter basis, of a total animal diet. In one suchembodiment, distillers meal as described herein is used as a CPsupplement in a cattle diet, and the distillers meal providesapproximately 5% to 20% by weight, on a dry matter basis, of the totaldiet. In yet another such embodiment, distillers meal as describedherein is used as a CP supplement in a cattle diet, and the distillersmeal provides approximately 5% to 15% by weight, on a dry matter basis,of the total diet. In still yet another such embodiment, distillers mealas described herein is used as a CP supplement in a cattle diet, and thedistillers meal provides approximately 10% to 15% by weight, on a drymatter basis, of the total diet. In yet another such embodiment,distillers meal as described herein is used as a CP supplement in acattle diet, and the distillers meal provides approximately 10% to 12%by weight, on a dry matter basis of the total diet. In another suchembodiment, distillers meal as described herein is used as a CPsupplement in a cattle diet, and the distillers meal providesapproximately 7% to 12% by weight, on a dry matter basis, of the totaldiet. In each of the preceding embodiments, where the distillers meal isfed to cattle, the distillers meal may be corn distillers meal asdescribed herein and the cattle may be finishing cattle.

In another embodiment, distillers meal as described herein may be usedin feeding dairy cattle. Where corn distillers meal is used as a dairycattle feed, it may be provided at, for examples, up to approximately30%, approximately 5% to 30%, approximately 5% to 25%, approximately 5%to 20%, approximately 5% to 15%, approximately 10% to 15%, approximately15% to 20%, approximately 15% to 25%, approximately 15% to 30%,approximately 10% to 20%, approximately 10% to 25%, approximately 20% to25%, or approximately 25% to 30% by weight, on a dry matter basis, ofthe total diet. In each of the exemplary embodiments, where thedistillers meal is fed to dairy cattle, the distillers meal may corndistillers meal as described herein.

In another embodiment, distillers meal as described herein is used as afeed supplement for cattle to achieve a desired F/G ratio. As it is usedherein, the term “F/G ratio” refers to the ratio of pounds of feed perpound of daily gain. In one embodiment, distillers meal as describedherein is used as a cattle feed supplement to achieve an F/G ratio of4.5 or less after 4 weeks of feeding. In another embodiment, distillersmeal as described herein is used as a cattle feed supplement to achievean F/G ratio of 5.0 or less after 8 weeks of feeding. In yet anotherembodiment, distillers meal as described herein is used as a cattle feedsupplement to achieve an F/G ratio of 6.5 or less after 12 weeks offeeding. In yet another embodiment, distillers meal as described hereinis used as a cattle feed supplement to achieve an F/G ratio of 7.0 orless after 16 weeks of feeding. In yet another embodiment, distillersmeal as described herein is used as a cattle feed supplement to achievean F/G ratio of 6.5 or less through 18 weeks of feeding. In each of theembodiments described herein pertaining to use of distillers meal as afeed supplement in cattle to achieve a desired F/G ratio, the distillersmeal may be de-corn distillers meal, the cattle may be, for example,finishing cattle, and the corn distillers meal may provide, for example,approximately 5% to 15%, 5% to 10%, 7%-12%, or 10% to 12% by weight, ona dry matter basis, of the total diet. Alternatively, in each of theembodiments described herein pertaining to use of distillers meal as afeed supplement in cattle to achieve a desired F/G ratio, the distillersmeal may be corn distillers meal, the cattle may be, for example,finishing cattle, and the corn distillers meal may provide, for example,approximately 5%, 6%, 7%, 8%, 9%, 10%, 11%, 12%, 13%, 14%, or 15% byweight, on a dry matter basis, of the total diet.

In yet another embodiment, distillers meal as described herein may beused as a feed supplement for cattle to achieve a desired average dailygain (ADG). In one embodiment, distillers meal as described herein isused as a cattle feed supplement to achieve an ADG of 4.0 lbs or greaterafter 4 weeks of feeding. In another embodiment, distillers meal asdescribed herein is used as a cattle feed supplement to achieve an ADGof 4.5 lbs or greater after 8 weeks of feeding. In yet anotherembodiment, distillers meal as described herein is used as a cattle feedsupplement to achieve an ADG of 3.5 lbs or greater after 12 weeks offeeding. In yet another embodiment, distillers meal as described hereinis used as a cattle feed supplement to achieve and maintain an ADG of3.5 lbs or greater through 16 weeks of feeding. In yet anotherembodiment, distillers meal as described herein is used as a cattle feedsupplement to achieve and maintain an ADG of 3.5 lbs or greater through18 weeks of feeding. In yet another embodiment, distillers meal asdescribed herein is used as a cattle feed supplement to achieve an ADGof 4.0 lbs or greater after 18 weeks of feeding. In each of theembodiments described herein pertaining to use of distillers meal as afeed supplement in cattle to achieve a desired ADG, the distillers mealmay be corn distillers meal, the cattle may be, for example, finishingcattle, and the corn distillers meal may provide, for example,approximately 5% to 15%, 5% to 10%, 7%-12%, or 10% to 12% by weight, ona dry matter basis, of the total diet. Alternatively, in each of theembodiments described herein pertaining to use of distillers meal as afeed supplement in cattle to achieve a desired ADG, the distillers mealmay be corn distillers meal, the cattle may be, for example, finishingcattle, and the corn distillers meal may provide, for example,approximately 5%, 6%, 7%, 8%, 9%, 10%, 11%, 12%, 13%, 14%, or 15% byweight, on a dry matter basis, of the total diet.

The distillers meal may be provided in meal form or in pellet form orother forms useful for feeding livestock or poultry, as would berecognized in the art. The distillers meal may also be premixed withother desired ingredients of a livestock or poultry diet and providedfor use in a ready-to-feed form. In addition to distillers meal asdescribed herein, livestock and poultry diets as described herein mayfurther include, for example, desired percentages of other componentssuch as feed corn, corn meal, soybean meal, urea, hay, pre-preparedcattle feeds, protein supplements, mineral supplements, liquidsupplements and other feed components as known and used by those ofskill in the art. Other acceptable materials used in livestock andpoultry feed may include, for example, soybeans, soy hulls, soybeanprotein derivatives, wheat, wheat middling, wheat straw, alfalfa, sugarbeet tailings, sugar beet pulp, sugar beets, corn stalks, corn cobs,popcorn husks, sweet bran, silage, meat and bone meal, molasses, oats,oat straw, barley, barley straw, sunflower seeds and hulls, milo, andwild grass, cottonseed by-products, such as delinted whole cottonseed,fuzzy cottonseed, and by-products of other oil seeds.

EXAMPLES Example 1

Corn DDGS from a dry grind corn ethanol biorefinery were subjected to ahexane extraction process as described herein to achieve corn distillersmeal having desired nutritional qualities. A selection of thenutritional properties of the corn distillers meal are provided in Table1.

TABLE 1 Nutritional Properties of De-oiled Corn Grain DDGs 06S-05686 AsReceived 100% Dry DDG DE-OILED PLANT TRIAL Basis Matter Basis TotalMoisture, % 4.00 0.000 Total Dry Matter, % 96.0 100 Karl FisherMoisture, % 2.63 Crude Protein, Combustion, % 32.0 33.3 Crude Fat(Diethyl Ether Extract), % 3.03 3.16 Ash, % 4.66 4.85 Crude Fiber,Crucible Method, % 7.06 7.35 Acid Detergent Fiber, % 11.5 12.0 NeutralDetergent Fiber, % 25.6 26.7 Nitrogen Free Extract, % 49.0 51.0Alanine - Total, % 2.26 2.35 Ammonia - Total, % 0.700 0.729 Arginine -Total, % 1.24 1.29 Aspartic Acid - Total, % 2.36 2.46 Glutamic Acid -Total, % 5.13 5.34 Glycine - Total, % 1.17 1.22 Histidine - Total, %0.704 0.733 Isoleucine - Total, % 0.838 0.873 Leucine - Total, % 3.573.72 Lysine - Total, % 0.735 0.766 Phenylalanine - Total, % 1.41 1.47Proline - Total, % 2.50 2.60 Serine - Total, % 1.58 1.65 Threonine -Total, % 1.13 1.18 Tyrosine - Total, % 1.20 1.25 Valine - Total, % 1.211.26 TDN (Proximate), % 75.7 78.9 NE/Lactation (Proximate), Mcal/lb 0.790.82 NE/Maintenance (Proximate), Mcal/lb 0.83 0.86 Metabolizable Energy,kcal/lb 1180 1230 NE/Gain (Proximate), Mcal/lb 0.55 0.57

Example 2

Corn DDGS from a dry grind corn ethanol biorefinery were subjected to ahexane extraction process as described herein to achieve corn distillersmeal having desired physical and nutritional properties. A selection ofthe physical and nutritional properties of the corn distillers meal areprovided below in Table 3 and Table 4.

The corn distillers meal was then subjected to two different pelletingprocesses. The pelleting conditions are described below in Table 2, with“Run 1” representing the first pelleting process and “Run 2”representing the second pelleting process. A selection of the physicaland nutritional properties of the pelleted corn distillers meal producedin the two pelleting runs are provided below in Table 3 and Table 4.

TABLE 2 Processing Conditions used for Pelleting Distillers Meal Run 1Run 2 Mean St Dev Mean St Dev Pellet Mill CPM # 3016 CPM # 3016 DieLength/Die Diameter 2.25″/3/16″ 2.25″/3/16″ Mill discharge temp (° F.)170.22 3.87 172.90 3.32 System motor load (kW) 39.39 7.81 29.82 1.91Throughput (tons/hr) 1.91 0.39 1.13 0.04

TABLE 3 Physical Properties of Distillers Meal and Pelletized DistillersMeal Distillers Pellets Meal Run 1 Run 2 Property Mean St Dev Mean StDev Mean St Dev Moisture content (%, wb) 10.89 0.25 7.64 0.35 7.52 0.27Water activity (—) 0.48 0.00 0.36 0.00 0.35 0.00 Particle size-GMD (mm)0.65 — — — — — Particle size-GSD (mm) 1.87 — — — — — Thermal-conductivity (W/mC) 0.08 0.00 — — — — Thermal - diffusivity (mm²/s)0.12 0.00 — — — — Color - L (—) 45.10 0.99 35.45 0.49 34.62 0.84 Color -a (—) 9.00 0.21 7.05 0.42 7.03 0.28 Color - b (—) 19.37 0.40 14.05 0.6313.74 0.46 Fines (%) — — 10.00 3.00 3.00 0.00 Pellet Durability Index(%) — — 61.97 1.82 71.98 2.22 Bulk density (lb/ft³) 30.71 0.06 31.960.35 35.04 0.12 Angle of repose (°) 14.99 0.51 19.82 1.66 17.87 0.49Unit density (kg/m³) — — 727.17 97.21 605.70 98.64

TABLE 4 Nutritional Properties of Distillers Meal and PelletizedDistillers Meal De-oiled Pellets DDGS Run 1 Run 2 Property Mean St DevMean St Dev Mean St Dev Moisture 10.89 0.25 7.64 0.35 7.52 0.27 content(%, wb) Protein (%, db) 34.35 0.07 34.15 0.07 33.50 0.14 Fiber (%, db)8.20 0.14 8.20 0.28 8.00 0.28 Fat (%, db) 2.65 0.07 4.95 0.07 5.10 0.14Ash (%, db) 5.01 0.03 4.97 0.09 4.98 0.01 Nitrogen Free 49.75 0.21 47.750.49 48.45 0.35 Extract (%, db)

Example 3

In the following example, corn distillers meal as described herein wasused as a feed supplement in finishing cattle diets. The performance ofthe diets supplemented with the corn distillers meal was compared to acontrol diet that did not utilized corn distillers meal as a feedsupplement.

Three finishing cattle diets, including a control diet lacking corndistillers meal and two finishing cattle diets including a supplement ofcorn distillers meal, were designed for the study. Substitutions wereiso-nitrogenous where corn distillers meal replaced corn, soy bean mean(“SBM”) and urea. As shown in Table 5, the three diets all contained afixed amount of a liquid supplement formulation including urea, monensinand tylosin, and other micro-ingredients at the same concentration forall three diets. The three diets were: 1) SBM/urea as a control diettypical for feed lots; 2) corn distillers meal replacing SBM and dryurea; and 3) corn distillers meal/SBM where corn distillers mealreplaced 90% of the SBM and the dry urea.

TABLE 5¹ Diet 2 Diet 3 Corn 10% SBM Diet 1 Distillers 90% Corn SBM MealDistillers Meal Grass Hay % 4.04 4.05 4.05 Whole shelled corn %² 53.7347.45 47.84 High moisture ear corn % 32.33 32.43 32.41 Liquid supplement%² 4.47 4.48 4.48 Pelleted supplement % 5.44 11.59 11.23 SBM³ (5.02) —(1.12) Urea³ (0.42) — — Corn distillers meal³ — (11.59) (10.11) Drymatter (DM)% 74.93 74.84 74.88 Crude protein (CP)% 13.28 13.20 13.24Neutral Detergent Fiber 14.43 18.40 17.93 (NDF) %^(a) Ash %^(a) 2.502.68 2.67 ¹All values except dry matter (DM) on DM basis. ²Contained 45%CP from Urea; 678 g/T monensin; 164 g/T tylosin; fortified with mineralsand vitamins to meet or exceed NRC requirements. ³Values in parenthesesare totaled as Pelleted Supplement. ^(a)Treatments differ (P < 0.01)

The cattle had been in the feedlot for more than 60 days prior tobeginning the study. There were 48 steers randomly assigned to each ofthe three diets, 6 steers in 8 pens for each diet. The total number ofsteers was 144. Cattle were fed twice daily in equal proportions overthe course of the 132 day study. All individual steer body weights weremeasured in the morning before feed was delivered. There was no fastingor water deprivation. Step-up diets were used to acclimatize the steersto the study diets and the final diets were first offered on day 22 ofthe study. On day 28 of the study, the steers were implanted withRevalor® S, available from Intervet Inc.

The data for average daily gain (ADG), dry matter intake (DMI), andpounds feed/average daily gain (F/G) were collected and compiled alongwith body weight and feed records. For all interim period reporting,performance calculations were made using unshrunk body weights. Forcumulative performance calculations, final body weight (BW) was shrunkby 3%. The final live body weight of each of the study animals wascalculated as hot carcass weight (HCW) divided by a constant dressingpercentage of 62.5%. On day 132 of the feedlot study, only the morningfeed was delivered and the cattle were harvested the following morning.

Results

The results of this study show that corn distillers meal can be used asa feed supplement and source of CP without any loss of carcass qualityor steer health. More particularly, the study indicates that corndistillers meal may be used as a feed supplement for carbohydrates,protein, as well as non-protein nitrogen (NPN) containing compounds. Asshown by Table 5, the corn distillers meal was used in Diet 2 and Diet 3as a substitute for at least part of the CP from SBM, along withapproximately 0.42% by weight of urea, and approximately 6.5% by weightof dietary corn, relative to the control diet.

Referring to Table 6, steers fed corn distillers meal had significantlyhigher (P<0.05) initial ADG at day 28 and day 56, when compared tosteers fed the control diet. The corn distillers meal diet containedmore neutral detergent fiber than the control diet and digesta retentiontime and water holding may therefore be increased. Diet 2 and Diet 3 hada marginally higher DMI, relative to the control diet. However, as shownin Table 6, the slightly higher DMI did not correspond to significantdifferences in ADG for the study.

With continued reference to Table 6, after day 112, the ADG was verysimilar for each of the diets at each of the testing intervals. Also,the F/G ratio of the de-oiled diets was comparable to the SBM/ureacontrol diet—ranging from approximately 6.67-6.83 pounds on day 112 andfrom approximately 5.91-6.13 pounds on day 132.

TABLE 6 Treatment Diet 2 Diet 3 Diet 1 Corn SBM/Corn SBM/urea DistillersMeal Distillers Meal SEM Initial BW lb  769  769  771 2.0 Day 28 BW lb 887^(b)  891^(b)  903^(a) 2.7 ADG lb   4.21^(b)   4.38^(b)   4.71^(a)0.087 DMI lb  17.15^(b)  17.47^(ab)  17.63^(a) 0.118 F/G   4.07^(b)  4.00^(b)   3.74^(a) 0.104 Day 56 BW lb 1022 1044 1033 6.1 ADG lb  4.82^(a)   5.44^(b)   4.65^(a) 0.195 DMI lb  22.17  23.17  22.70 0.393F/G   4.62^(ab)   4.26^(a)   4.93^(b) 0.166 Day 84 BW lb 1137^(b)1155^(a) 1147^(b) 4.6 ADG lb   4.12   3.98   4.07 0.132 DMI lb  24.02 24.55  24.11 0.273 F/G   5.84   6.19   5.97 0.224 Day 112 BW lb1244^(a) 1264^(b) 1256^(a) 6.3 ADG lb   3.82   3.90   3.89 0.143 DMI lb 25.50^(a)  26.51^(b)  25.81^(a) 0.149 F/G   6.76   6.83   6.67 0.258Day 132 BW lb 1331 1350 1339 7.8 ADG lb   4.33   4.31   4.16 0.216 DMIlb  25.38  25.76  25.39 0.420 F/G   5.91   6.10   6.13 0.236 ^(ab)Meanswithout common superscripts differ (P < 0.05)

Tables 7 and 8 show the cumulative data collected during the study andthe carcass traits of the harvested steers. As shown in Table 6, theslightly higher DMI for the corn distillers meal substituted diets didnot correspond to significant differences in diet ADG for the length ofthe study. The cumulative DMI was less than 3% greater for corndistillers meal in contrast to the SBM/urea control diet. As shown inthe bottom half of Table 7, the carcass adjusted final body weight, asderived from the hot carcass weight (HCW), were very similar among thetest diets. The final F/G ratio, carcass adjusted, was 5.83 lbs in theSBM/urea control diet. The F/G ratio in the corn distillers meal dietswas 5.81 lbs and 5.76 lbs. The comparable F/G ratios indicate that thecorn distillers meal substituted diets are just as effective as thecontrol diet for inducing a steadily increasing body weight for thelength of the study. Moreover, as shown in Table 5, the carcass traitsof the corn distillers meal diet were similar to the carcass traits ofthe control diet.

TABLE 7 Treatment Diet 2 Diet 3 Diet 1 Corn Distillers SBM/Corn SBM/ureaMeal Distillers Meal SEM Final BW¹ lb 1291 1310 1299 7.6 ADG lb 3.954.10 4.00 0.054 DMI lb 22.69 23.35 22.99 0.218 F/G 5.75 5.70 5.75 0.050Carcass adjusted Final BW² 1283 1298 1298 7.6 ADG 3.90 4.02 3.99 0.047F/G 5.83 5.81 5.76 0.063 ¹3% pencil shrink applied. ²Derived from HCWlb/0.625.

TABLE 8 Diet Diet 2 Diet 3 Diet 1 Corn Distillers SBM/Corn SBM/urea MealDistillers Meal SEM Dress %² 62.1 62.0 62.5 0.26 HCW lb 802 812 812 4.1REA in.² 12.49 12.69 12.87 0.182 KPH % 2.35 2.31 2.28 0.037 MarblingScore³ 5.63 5.47 5.78 0.112 Yield Grade 3.33 3.30 3.40 0.069 Choice &Prime % 81.0 79.5 80.2 5.61 ¹Pen basis. ²Includes 3% shrink of finallive weight. ³4.00 = Select°; 5.0 = Small°.

Example 4

In the following example, corn DDGS from a dry grind corn ethanolbiorefinery were subjected to a hexane extraction process as describedherein to achieve crude corn oil. More particularly, corn DDGS wereobtained from the removal of ethyl alcohol by distillation from theyeast fermentation of corn by condensing and drying the solids of theresultant whole stillage by methods employed in the grain distillingindustry using the dry milling process. The crude corn oil is furtherremoved from the corn DDGS by hexane extraction for use as food gradecorn oil or for the production of biodiesel and glycerin. A selection ofthe nutritional properties of the extracted crude corn oil are providedin Table 9.

TABLE 9 Oil Extracted From DDGS 100% As Received Basis Dry Matter BasisKarl Fisher Moisture % 1.40 — Crude Protein % 0.560 0.56 Total Nitrogen% 0.0895 0.089 Ash % 0.0800 0.6 Calcium % 0.00800 0.008 Cobolt, ug/g(ppm) — <0.1 Copper, ug/g (ppm) — <2.0 Iron, ug/g (ppm) 14.9 14.9Magnesium % 0.00500 0.005 Molybdenum, ug/g (ppm) — <0.20 Manganese, ug/g(ppm) — <1.0 Phosphorus % 0.0180 0.018 Potassium % 0.00600 0.006 Sodium% 0.00300 0.003 Sulfur % 0.0190 0.019 Zinc, ug/g (ppm) 2.40 2.40 FreeFatty Acids as Oleic % 9.9 9.9 Free fatty acid value is expressed aspercent oleic acid. Free fatty acid value can also be expressed as acidvalue. In this case, 9.9% free fatty acid (as oleic) is equivalent to19.7 acid value [19.7 milligrams potassium hydroxide (KOH) to neutralize1 gram of oil].

It should be emphasized that the described embodiments of thisdisclosure are merely possible examples of implementations and are setforth for a clear understanding of the principles of this disclosure.Many variations and modifications may be made to the describedembodiments of this disclosure without departing substantially from thespirit and principles of this disclosure. All such modifications andvariations are intended to be included herein within the scope of thisdisclosure and protected by the following claims.

1. A single facility for solvent extraction of distillers dried grainswith solubles comprising: a solvent extraction facility configured toextract crude plant oil from the distillers dried grains with solubles,thereby producing distillers meal, wherein the solvent extractionfacility is configured to extract crude plant oil from distillers driedgrains with solubles using a hexane extraction process, therebyproducing distillers meal comprising a crude protein content rangingfrom approximately 28% to approximately 35% by weight on a dry matterbasis, a crude fat content ranging from approximately 0.5% toapproximately 6% by weight on a dry matter basis, a neutral detergentfiber content ranging from approximately 25% to approximately 35% byweight on a dry matter basis, and an acid detergent fiber contentranging from approximately 10.0% to approximately 20.0% by weight on adry matter basis.
 2. The single facility for solvent extraction of claim1, wherein the crude plant oil is further processed bytransesterification to produce biodiesel and glycerin.
 3. The singlefacility for solvent extraction of claim 1, wherein the crude plant oilis further processed by filtering and bleaching to produce food gradeoil.
 4. (canceled)
 5. A single facility for solvent extraction ofdistillers dried grains with solubles comprising: a solvent extractionfacility configured to extract crude plant oil from distillers driedgrains with solubles using a hexane extraction process, therebyproducing distillers meal, wherein the crude plant oil comprisesapproximately 1% to approximately 15% by weight free fatty acids on adry matter basis, and no more than 0.2% ash by weight on a dry matterbasis.
 6. Distillers meal comprising: a crude protein content rangingfrom approximately 28% to approximately 35% by weight on a dry matterbasis; a crude fat content ranging from approximately 0.5% toapproximately 6% by weight on a dry matter basis; a neutral detergentfiber content ranging from approximately 25% to approximately 35% byweight on a dry matter basis; and an acid detergent fiber contentranging from approximately 10% to approximately 20% by weight on a drymatter basis.
 7. The distillers meal of claim 6, wherein the crudeprotein content is approximately 31% to approximately 33% by weight on adry matter basis, the crude fat content is approximately 1% toapproximately 4% by weight on a dry matter basis, the neutral detergentfiber content is approximately 28% to approximately 34% by weight on adry matter basis, and the acid detergent fiber content is approximately11% to approximately 17% on a dry matter basis.
 8. The distillers mealof claim 6, wherein the distillers meal is corn distillers meal producedby solvent extraction of corn distillers dried grains with solubles. 9.The distillers meal of claim 8, wherein the corn distillers meal isproduced by hexane extraction of corn distillers dried grains withsolubles.
 10. The distillers meal of claim 9, wherein the hexaneextracted corn distillers meal comprises approximately 28% toapproximately 35% by weight crude protein on a dry matter basis,approximately 1% to approximately 4% by weight crude fat on a dry matterbasis, approximately 28% to approximately 34% by weight neutraldetergent fiber content on a dry matter basis, and approximately 11% toapproximately 17% by weight acid detergent fiber on a dry matter basis.11. The distillers meal of claim 6, further comprising nutritionalcharacteristics selected from the group consisting of approximately 0.70Mcal/lb to approximately 0.85 Mcal/lb net energy lactation,approximately 0.75 Mcal/lb to approximately 0.89 Mcal/lb net energymaintenance, approximately 0.50 Mcal/lb to approximately 0.60 Mcal/lb ofnet energy gain, or any combinations thereof.
 12. Crude plant oilextracted from distillers dried grains comprising: free fatty acids inan amount ranging from approximately 1% to approximately 15% by weighton a dry matter basis.
 13. The crude plant oil of claim 12, wherein thecrude plaint oil is extracted from corn distillers dried grains withsolubles using hexane extraction.
 14. The crude plant oil of claim 13,further comprising: crude protein in an amount ranging no more thanabout 1% by weight on a dry matter basis; phosphorus in an amountranging from approximately 0.01% to approximately 0.04% by weight on adry matter basis; and sulfur in an amount ranging from approximately0.02% to approximately 0.05% by weight on a dry matter basis.
 15. Ananimal feed comprising: distillers meal in an amount ranging fromapproximately 5% to approximately 75% by weight of the total feed on adry matter basis; wherein the distillers meal is corn distillers mealand comprises approximately 28% to approximately 35% by weight crudeprotein on a dry matter basis, approximately 0.5% to approximately 6% byweight crude fat on a dry matter basis, approximately 25% toapproximately 35% by weight neutral detergent fiber content on a drymatter basis, and approximately 10% to approximately 20% by weight aciddetergent fiber on a dry matter basis.
 16. (canceled)
 17. The animalfeed of claim 15, wherein the corn distillers meal further comprisesnutritional characteristics selected from the group consisting ofapproximately 0.70 Mcal/lb to approximately 0.85 Mcal/lb net energylactation, approximately 0.75 Mcal/lb to approximately 0.89 Mcal/lb netenergy maintenance, approximately 0.50 Mcal/lb to approximately 0.60Mcal/lb of net energy gain, or any combinations thereof.
 18. The animalfeed of claim 17, wherein the corn distillers meal comprisesapproximately 5% to approximately 75% by weight of the total feed on adry matter basis.
 19. The animal feed of claim 17, wherein the corndistillers meal comprises approximately 5% to approximately 40% byweight of the total feed on a dry matter basis.
 20. The animal feed ofclaim 19, wherein the corn distillers meal comprises approximately 10%to approximately 30% by weight of the total feed on a dry matter basis.21. A method of feeding animals, the method comprising: providing ananimal feed to the animals; supplementing the animal feed withdistillers meal in an amount ranging from approximately 5% toapproximately 75% by weight of the total animal feed, on a dry matterbasis; and wherein the distillers meal comprises a crude protein contentranging from approximately 28% to approximately 35% by weight on a drymatter basis.
 22. The method of claim 21, wherein the distillers meal iscorn distillers meal and comprises a neutral detergent fiber contentranging from approximately 25% by weight to approximately 35% by weight,and wherein the corn distillers meal comprises a crude fat contentranging from approximately 0.5% by weight to approximately 6% by weight.23. The method of claim 21, wherein the distillers meal is corndistillers meal and providing an animal feed to the animals comprisesproviding the animal feed to cattle.
 24. The method of claim 23, whereinsupplementing the animal feed with the corn distillers meal produces, inthe cattle, a ratio of total pounds of feed per average daily gain, orF/G ratio, ranging from approximately 7 lbs. to approximately 3 lbs, orless.
 25. The method of claim 24, wherein supplementing the animal feedwith the corn distillers meal produces, in the cattle, a ratio of totalpounds of feed per average daily gain, or F/G ratio, selected from anF/G ratio of 4.5 lbs. or less after 4 weeks of feeding, 5.0 lbs or lessafter 8 weeks of feeding, 6.5 lbs or less after 12 weeks of feeding, 7.0lbs. or less after 16 weeks of feeding, and 6.5 lbs or less through 18weeks of feeding.
 26. The method of claim 23, wherein supplementinganimal feed with the corn distillers meal produces an average daily gainin the cattle selected from an average daily gain of 4.0 lbs or greaterafter 4 weeks of feeding, 4.5 lbs. or greater after 8 weeks of feeding,3.5 lbs or greater after 12 weeks of feeding, 3.5 lbs. or greaterthrough 16 weeks of feeding, 3.5 lbs or greater through 18 weeks offeeding, and 4.0 lbs or greater after 18 weeks of feeding.
 27. The crudeplant oil of claim 12, further comprising nitrogen in an amount no morethan approximately 0.5% by weight on a dry matter basis; and ash in anamount no more than approximately 0.2% by weight on a dry matter basis.28. The single facility for solvent extraction of claim 5, wherein thecrude plant oil is further processed by transesterification to producebiodiesel and glycerin.
 29. The single facility for solvent extractionof claim 5, wherein the crude plant oil is further processed byfiltering and bleaching to produce food grade oil.